Regenerative adsorbent heat pump

ABSTRACT

A regenerative adsorbent heat pump process and system is provided which can regenerate a high percentage of the sensible heat of the system and at least a portion of the heat of adsorption. A series of at least four compressors containing an adsorbent is provided. A large amount of heat is transferred from compressor to compressor so that heat is regenerated. The process and system are useful for air conditioning rooms, providing room heat in the winter or for hot water heating throughout the year, and, in general, for pumping heat from a low temperature to a higher temperature.

ORIGIN OF INVENTION

The invention described herein was made in the performance of work undera NASA Contract, and is subject to the provisions of Public Law 96-517(35 USC 202) in which the contractor, has elected to retain title in theUnited States.

RELATED U.S. APPLICATION DATA

U.S. National Phase of International Ser. No. PCT/US91/07173 havingInternational Filing Date Sep. 30, 1991, which is a Continuation-in-Partof U.S. Ser. No. 598,525, Oct. 16,1990, U.S. Pat. No. 5,046,319.

BACKGROUND OF THE INVENTION

1. Technical Field

This invention is directed towards regenerative heat pump system andmethod using a working fluid or refrigerant and an adsorbent material.

2. Discussion of the Invention

Heat pumps using solid adsorbent beds are known as shown by U.S. Pat.No. 4,610,148, U.S. Pat. No. 4,637,218 and U.S. Pat. No. 4,694,659 whichuse zeolite as the adsorbent and water as the working fluid. In generalsince adsorbents take up the working fluid when cooled and desorb theworking fluid when heated, adsorbent heat pumps are said to be heatdriven. Often in adsorbent heat pumps two beds of sorbents are used, oneto adsorb the working fluid while the other bed is desorbing the workingfluid. Alternate heating and cooling of the beds is the conventionalprocedure. When used in air conditioning, heat from an interior room maybe used to evaporate the working fluid in an evaporator with heatrejection to the environment at ambient temperatures.

In all of such systems the efficiency of the apparatus is measured byits coefficient of performance or "COP". By the term "COP" as usedherein is meant the ratio of heating or cooling work performed dividedby the amount of power required to do the work. Since cooling COP_(S),or COP_(CS), are generally lower than heating COP_(S), or COPM_(S), manysystems are rated on their cooling COP_(S).

U.S. Pat. No. 4,637,218 mentions cooling COP_(S) between 1 and 2 andheating COP_(S) between 2 and 3 both of which are apparently idealvalues since it is later stated that in practice for the heating modethe COP is less but with proper design is nevertheless within about 80%of the theoretical value, that is, about 2.4. In U.S. Pat. No. 4,637,218a hot coolant is pumped from a hot 204.4° C. sorbent compressor to acooler 37.8° C. sorbent compressor, while at the same time cold coolantis pumped from the cooler sorbent compressor to the hotter sorbentcompressor. Both compressors exchange heat yielding a typical heatregeneration efficiency of about 80%. The remainder of the heat issupplied by a boiler at about 204° C. Water vapor as the working fluidis desorbed from the hot sorbent at, a relatively high pressure whilethe cold sorbent adsorbs the working fluid at a relatively low pressure.Expansion of the working fluid from the higher pressure to the lowerpressure creates net cooling at 4.4° C.

U.S. Pat. No. 4,610,148 reports a theoretical heating COP of about 3 anda cooling COP of about 2, and, a calculated operating COP_(H) of about2.6 and a calculated operating COP_(C) of about 1.6.

FIG. 3 of U.S. Pat. No. 4,694,659, which is concerned with a dualsorbent bed heat pump, shows heating and cooling COP's as a function ofa dimensionless thermal wavelength parameter which at a value of about0.5 corresponds to a heating COP of about 2.7 and a cooling COP of about1.7.

Cryogenic cooler systems for sorption refrigerators using a sorptioncompressor, a heating/cooling loop and a Joule-Thomson expansion valve,or "J-T" valve, with methane as a refrigerant gas and charcoal as theadsorbent, are disclosed in articles entitled "High Efficiency SorptionRefrigerator Design", and "Design and Component Test Performance of anEfficient 4 W, 130 K Sorption Refrigerator" in Advances In CryogenicEngineering, Vol. 35, Plenum Press, New York, 1990. Desorption occurs at4.46 MPa (646 psia), i.e. P_(H), and adsorption at 0.15 MPa (22 psia),i.e. P_(L), or a pressure ratio of about 30, i.e, P_(H) /P_(L) =30.Methane is expanded from 4.46 MPa to 0.15 MPa to achieve cooling below130K (-143° C.). The sorbent is heated from 240K (-33° C.) to 600K (327°C.) to desorb the methane. However based on data from another source ithas been noted that for this cryogenic cooler system the sorbent must beheated from 240K to 415K (142° C.) before any methane is desorbed, andthe sorbent must be cooled from 600K (327° C.) to 320K (47° C.) beforeany methane is adsorbed. The temperature ranges with high thermalcapacitance, which accounts for the heat of adsorption, during heatingis from 415K to 800K, and during cooling is from 320K to 240K. Since theheating high thermal capacitance temperature range does not overlap thecooling high thermal capacitance temperature range, none of the heat ofadsorption can be recovered for use in the system, and as a consequencethe heat of adsorption must be rejected entirely from the system. In theabove mentioned methane/charcoal cryogenic refrigerator, the system'shigh pressure ratio of about 30 essentially precludes regeneration ofthe heat of adsorption. Usually in systems with high pressure ratios,i.e. P_(H) /P_(L) ratios over about 10, none of the heat of adsorptioncan be regenerated. By the term "sensible heat" as used herein is meantthe "mass" times "specific heat" times "temperature change". Thereforeunless otherwise specified, the term "sensible heat" as used herein doesnot include latent heat or heat of adsorption.

In order to improve system efficiency and COP_(S) it therefore would bedesirable to regenerate at least a portion of the heat of adsorption.

SUMMARY OF THE INVENTION

It is an objective of this invention to provide a system and processimproving the efficiency of regenerative sorbent heat pump operations.It is also an object of this invention to provide a system and processfor regenerating at least a portion of the heat of .adsorption. Anotherobject of this invention is to provide a regenerative sorbent heat pumpsystem and process having an enhanced coefficient of performance. Stillanother object of this invention is to provide a regenerative sorbentheal pump system and process which can be used for cooling rooms of abuilding. Yet another object of this invention is to provide suchsystems and processes which can operate using working fluids orrefrigerants having very low or no atmospheric ozone-depletion-potentialor "ODP". It is a further object of this invention to provide a systemwhich can be used for heating and cooling rooms and buildings in whichthe heating can be for comfort or space heating in the winter or forproducing hot water year around.

Accordingly there is provided by the principles of this invention aregenerative sorbent heat pump process for cooling a chamber, room or aninterior space and for simultaneously regenerating at least a portion ofthe heat of adsorption. This invention comprises confining a sorbent ina plurality of compressor zones, the number of compressor zones being atleast four; continuously introducing a working fluid vapor from anevaporation zone into at least one of the number of compressor zones andsorbing the working fluid vapor on the sorbent therein over apredetermined first or adsorption temperature range and a predeterminedfirst (low) pressure or P_(L) ; continuously desorbing working fluidvapor from the sorbent in at least one of the remaining number ofcompressor zones and removing working fluid vapor therefrom over apredetermined second or desorption temperature range which is higherthan the predetermined first temperature or adsorption range and at apredetermined second (high) pressure or P_(H) which is higher than thepredetermined first pressure. A part of the predetermined first oradsorption temperature range overlaps a part of the predetermined secondof desorption temperature range. The process further comprisescontinuously condensing working fluid vapor removed from at least one ofthe remaining number of the compressor zones at P_(H) and transferringheat from the working fluid to the environment thereby forming a workingfluid liquid; and continuously evaporating the working fluid liquid andforming the working fluid vapor in the evaporation zone at P_(L) bytransferring heat from an interior space to the evaporation zone therebycooling the interior space. Evaporation of the working fluid liquid cancomprise passing it across an expansion valve. The process alsocomprises continuously circulating a heat transfer fluid in series flowthrough the compressor zones and preventing the heat transfer fluid fromdirectly contacting the sorbent; and continuously removing heat from theheat transfer fluid and transferring it to the environment. The processincludes adding heat from a heat source to a predetermined one of thecompressor zones over a predetermined period of time; repeating the lastmentioned adding heat step sequentially in each of the compressor zones;continuously indirectly transferring heat from the sorbent in thecompressor zones which are sorbing working fluid vapor to the heattransfer fluid and from the heat transfer fluid to the sorbent in thecompressor zones which are desorbing working fluid vapor therebyregenerating heat; and, maintaining the P_(H) /P_(L) ratio sufficientlylow and the temperature overlap of the sorbing and desorbing operationsufficiently large so that at least a portion of the heat of adsorptionis regenerated.

In one embodiment the process further comprises maintaining the P_(H)/P_(L) ratio between about 1.1 and about 10, preferably between about1.1 and about 5, and especially between about 1.1 and about 3. In oneembodiment the process further comprises maintaining the P_(H) /P_(L)ratio sufficiently low that about 25% of the heat of adsorption isregenerated, preferably sufficiently low that about 50% of the heat ofadsorption is regenerated, more preferably sufficiently low that about70% of the heat of adsorption is regenerated, and especially preferablysufficiently low that about 100% of the heat of adsorption isregenerated.

In one embodiment the predetermined first or adsorption temperaturerange is from at least about -18° C. (0° F.) to no more than about 204°C. (400° F.), the predetermined second or desorption temperature rangeis from at least about 38° C. (100° F.) to no more than about 427° C.(800° F.), and, the adsorption and desorption temperature ranges overlapat least about 28 Celsius (50 Fahrenheit) degrees. In another embodimentthe predetermined first or adsorption temperature range is from at leastabout -18° C. (0° F.) to no more than about 204° C. (400° F.), thepredetermined second or desorption temperature range is from at leastabout 38° C. (100° F.) to no more than about 316° C. (600° F.), and, theadsorption and desorption temperature ranges overlap at least about 56Celsius (100 Fahrenheit) degrees. In a preferred embodiment thepredetermined first temperature range is from at least about -18° C. (0°F.) to no more than about 204° C. (400° F.) the predetermined secondtemperature range is from at least about 38° C. (100° F.) to no morethan about 260° C. (500° F.), and, the adsorption and desorptiontemperature ranges overlap at least about 56 Celsius (100 Fahrenheit)degrees. In an especially preferred embodiment the predetermined firsttemperature range is from at least about 10° C. (50° F.) to no more thanabout 177° C. (350° F.), the predetermined second temperature range isfrom at least about 38° C. (100° F.) to no more than about 232° C. (450°F.), and, the adsorption and desorption temperature ranges overlap atleast about 83 Celsius (150 Fahrenheit) degrees.

In one embodiment the continuous removal of heat from the heat transferfluid and transferring it to the environment comprises continuouslyremoving heat from the heat transfer fluid before it flows to apredetermined one of the compressor zones and transferring the removedheat to the environment. In a further embodiment the process comprisesrepeating the last mentioned heat removal step sequentially for each ofthe compressor zones.

In one embodiment the continuous removal of heat from the heat transferfluid and transferring it to the environment comprises continuouslyindirectly transferring heat from the first mentioned heat transferfluid before it flows to a predetermined one of the compressor zones toa second heat transfer fluid, and continuously removing heat from asecond heat transfer fluid by transferring heat to the environment. In afurther embodiment the process comprises repeating the last mentionedheat removal step sequentially for each of the compressor zones.

In still another embodiment the adding heat from a heat source to apredetermined one of the compressor zones over a predetermined period oftime is performed by adding heat to a third heat transfer fluid, and,indirectly transferring heat from the third heat transfer fluid to thefirst heat transfer fluid before it enters the predetermined one of thecompressor zones.

There is also provided by the principles of this invention aregenerative sorbent heat pump system comprising a working fluid beingoperable for being sorbed by a sorbent; a plurality of spaced apartcompressors. The number of compressors being at least four. Each of thecompressors has a sorbent contained within the compressor, an inlet forintroducing the working fluid for adsorption by the sorbent, an outletfor removing working fluid desorbed from the sorbent, and a heatconductive passageway having an inlet and an outlet. The heat conductivepassageway is for flowing a heat transfer fluid through the compressorand for indirectly transferring heat between the sorbent and the heattransfer fluid without the heat transfer fluid being in contact with thesorbent. The system further comprises means for removing hightemperature, high pressure working fluid vapor from each of thecompressors; condensing means for transferring heat from the workingfluid to the environment or a low temperature heat sink, and, forcondensing working fluid vapor to form a low temperature, high pressureworking fluid liquid. The system also comprises evaporating means forconverting low temperature, high pressure working fluid liquid to lowtemperature, low pressure working fluid vapor, and, for transferringheat from a low temperature source external of the system, includingrooms of a building, to the working fluid. Also included is liquidconveying means for conveying low temperature, high pressure workingfluid liquid from the condensing means to the evaporating means; and,vapor conveying means for conveying low temperature, low pressureworking fluid vapor into each of the compressors. The system has aplurality of indirect heat exchange means spaced apart from thecompressors. The number of indirect heat exchange means being equal tothe number of the compressors. Each of the indirect heat exchange meanshas a first channel for flowing a heat transfer fluid, and a secondchannel for flowing another heat transfer fluid. The channels beingisolated from fluid communication with each other. The first channelbeing in heat conductive communication with the second channel. Each ofthe channels has an inlet and an outlet. The system also includes atrain formed by connecting in alternating order, the first channels ofthe indirect heat exchange means to the heat conductive passageways. Thetrain has a train inlet the inlet of the first channel of thefirst-in-the-series of indirect heat exchange means of the train, and,as a train outlet the outlet of the heat conductive passageway of thelast-in-the-series of compressors of the train, the system also hasfirst pumping means for pumping a first heat transfer fluid around thefirst train. The outlet of the first pumping means being connected tothe train inlet and the train outlet being connected to the firstpumping means inlet. The system includes second pumping means forconveying a second heat transfer fluid; connecting means for connectingthe outlet of the second pumping means to the inlet of the secondchannel of each of the internal heat exchange means, and for connectingthe outlet of each of the second channels thereof to the second pumpingmeans inlet. Also included is flow control means for directing thesecond heat transfer fluid from the second pumping means to the secondchannel of a predetermined one of the indirect heat exchange means in apredetermined order thereby defining a flow cycle, and, thereby enablingheat transfer between the first heat transfer fluid in the first channelthereof and the second heat transfer fluid in the second channelthereof. Also included is primary heating means for heating each of thecompressors; and heat control means for controlling the heating periodof the primary heating means in each of the compressors thereby defininga heating cycle. Heat discharge means is included for transferring heatfrom the second heat transfer fluid flowing in the connecting means fromthe second channels to the second pump means, to the environment or alow temperature heat sink thereby providing a regenerative sorbent heatpump system.

In a further embodiment the system the further comprises heat exchangermeans for the indirect transfer of heat between the low temperature,high pressure working fluid liquid in the liquid conveying means and thelow temperature, low pressure working fluid vapor in the vapor conveyingmeans.

In another embodiment the system further comprises means forcoordinating the flow cycle and the heating cycle.

In still another embodiment the system also comprises auxiliary heatexchanger means for indirectly exchanging heat between the heat transferfluid flowing to the train and the heat transfer fluid flowing from thetrain. The system can also have means for transferring heat from theheat transfer fluid flowing from the train to a low temperature heatsink or to the environment.

In one embodiment the primary heating means comprises a heating devicein each of the compressors. In another embodiment the primary heatingmeans comprises a heating device between each of the compressors in thetrain and between the first pumping means outlet and the train inlet.These heating devices are for heating the first heat transfer fluidbefore it is introduced into the compressor for which it is intended, sothat the thusly heated heat transfer fluid thereby heats its intendedcompressor.

In another embodiment the primary heating means comprises a plurality ofsecond indirect heat exchange means spaced apart from the compressors.The number of second indirect heat exchange means being equal to thenumber of the compressors. Each of the second indirect heat exchangemeans having a first channel for flowing a heat transfer fluid, and asecond channel for flowing a heat transfer fluid. The channels thereofare isolated from fluid communication with each other. The first channelthereof being in heat conductive communication with the second channelthereof. Each of the channels thereof having an inlet and an outlet. Inthis embodiment the train includes the first channels of the secondindirect heat exchange means connected, relative to the heat conductivepassageways, in alternating order before each of the heat conductivepassageways. This embodiment also includes third pumping means forpumping a third heat transfer fluid; second connecting means forconnecting the outlet of the third pumping means to the inlet of thesecond channel of each of the second internal heat exchange means, andfor connecting the outlet of each of the second channels thereof to thethird pumping means inlet. Flow control means is also included fordirecting the third heat transfer fluid from the third pumping means tothe second channel of a predetermined one of the second indirect heatexchange means in a predetermined order thereby defining a second flowcycle, and, thereby enabling heat transfer between the first heattransfer fluid in the first channel thereof and the third heat transferfluid in the second channel thereof. The primary heating means alsoincludes a heating device in the second connecting means for heating thethird heat transfer fluid before it is introduced into the secondchannel of a predetermined one of the second indirect heat exchangemeans. The heat control means includes means for controlling the heatingdevices so that the temperature of the third heat transfer fluid iscontrolled.

In still another embodiment the pumping means conveys the heat transferfluid through a cooling loop and then through the train of heatconductive passageways and first channels of the indirect heat exchangemeans thereby cooling the compressors.

In one embodiment the pumping means divides the flow of heat transferfluid between a coolant loop and the train of heat conductivepassageways.

In yet another embodiment of this invention the system comprises firstconnecting means for forming a loop of heat conductive passageways byconnecting the outlet of one heat conductive passageway to the inlet ofanother heat conductive passageway and proceeding with suchinlet-to-outlet connections until the outlet of the last heat conductivepassageway is connected to the inlet of the first heat conductivepassageway thereby forming a loop of heat conductive passageways. Thisembodiment includes second connecting means for connecting the outlet ofthe pumping means to the inlet of each of the heat conductivepassageways; and third connecting means for connecting the outlet ofeach of the heat conductive passageways to the pumping means inlet.Additional flow control means is also included for directing the heattransfer fluid from the pumping means to the inlet of a predeterminedone of the heat conductive passageways, then around the loop passingthrough each of the heat conductive passageways only once, and then backto the pumping means. This embodiment also includes phase timing meansfor redirecting the heat transfer fluid after a predetermined timeinterval, from the pumping means to another one of the heat conductivepassageways thereby beginning a new phase, and for repeating suchredirecting after such predetermined time intervals to other of the heatconductive passageways, until the heat transfer fluid is directed fromthe pumping means to each of the heat conductive passageways therebycompleting a flow cycle. Heat discharge means is included fortransferring heat from the heat transfer fluid in the third connectingmeans to the environment or a low temperature heat sink.

In one embodiment the working fluid is selected from the groupconsisting of fluorine substituted ethanes, and, fluorine and chlorinesubstituted ethanes. In another embodiment the working fluid is selectedfrom the group consisting of 1,1,1,2-tetrafluoroethane or CF₃ CH₂ Freferred to herein as "R134a" 2-chloro-1,1,1,2-tetrafluoroethane or CF₃CHClF referred to herein as "R124", 1,1-dichloro-2,2,2-trifluoroethaneor CHCl₂ CF₃ referred to herein as "R123", ammonia and water.

In one embodiment the sorbent is selected from the group consisting ofactivated carbons, zeolites, silica gels and alumina. A preferredactivated carbon is known as AX-21.

In one embodiment the heat transfer fluid is selected from the groupconsisting of mixtures of diphenyl and diphenyl oxide,ortho-dichlorobenzene, ethylene glycol, methoxypropanol, and water.Examples of such heat transfer fluids are the Dowtherm™ fluids.

In one embodiment the number of compressor zones is four, and in apreferred embodiment the number of compressor zones is six. However, anynumber of compressors can be used if desired as long as the number is atleast four.

In one embodiment the process and system mat be used only forcompressing fluids, or only for separating mixed fluid constituents, butwithout necessarily pumping heat from a lower temperature heat source toa higher temperature heat source. Accordingly there is also provided bythe principles of this invention a regenerative sorbent heat pumpprocess for compressing a fluid and for simultaneously regenerating atleast a portion of the heat of adsorption comprising confining a sorbentin a plurality of compressor zones, the number of compressor zones beingat least four; introducing a working fluid vapor from an evaporationzone into at least one of the number of compressor zones and sorbing theworking fluid vapor on the sorbent therein over a predetermined firsttemperature range and a predetermined first pressure or P_(L) ;desorbing working fluid vapor from the sorbent in at least one of theremaining number of compressor zones and removing working fluid vaportherefrom over a predetermined second temperature range which is higherthan the predetermined first temperature range and at a predeterminedsecond pressure or P_(H) which is higher than the predetermined firstpressure, a part of the predetermined first temperature rangeoverlapping a part of the predetermined second temperature range;circulating a heat transfer fluid in series flow through the compressorzones and preventing the heat transfer fluid from directly contactingthe sorbent; removing heat from the heat transfer fluid and transferringit to the environment; adding heat from a heat source to a predeterminedone of the compressor zones over a predetermined period of time;repeating the adding heat step sequentially in each of the compressorzones; indirectly transferring heat from the sorbent in the compressorzones which are sorbing working fluid vapor to the heat transfer fluidand from the heat transfer fluid to the sorbent in the compressor zoneswhich are desorbing working fluid vapor thereby regenerating heat; and,maintaining the P_(H) /P_(L) ratio sufficiently low so that at least aportion of the heat of adsorption is regenerated.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a diagram of a first embodiment of this invention having atrain of six compressors and coolant loop.

FIG. 2 is a calculated temperature profile of the six compressors of theembodiment of FIG. 1.

FIG. 3 is isotherm data for R134a/AX-21 carbon sorbent system.

FIG. 4 is isotherm data for R124/AX-21 carbon sorbent system.

FIG. 5 is a diagram of a second embodiment of this invention having aseparate heating loop.

FIG. 6 is a diagram of a third embodiment of this invention having butone pump for a train of four compressors and a coolant loop.

FIG. 7 is a diagram of a fourth embodiment of this invention having butone pump for parallel flow to a train of compressors and a coolant loop.

FIG. 8 is a diagram of a fifth embodiment of this invention having aflow control system for both heating and cooling a train of compressors.

FIG. 9 is a calculated temperature profile of the four compressors ofthe embodiment of FIG. 6.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

Referring to FIG. 1, a block diagram for a regenerative sorbent heatpump system, generally designated by numeral 100, is shown for airconditioning, i.e. room heating and cooling. The system has sixcompressors 102A, 102B, 102C, 102D, 102E and 102F, having heatconductive passageways 104A, 104B, 104C, 104D, 104E and 104F,respectively, sorbent chambers 106A, 106B, 106C, 106D, 106E and 106F,respectively, and, chamber heating devices 108A, 108B, 108C, 108D, 10BEand 108F, respectively. The heat conductive passageways 104A-F arehermetically separated from chambers 106A-F, respectively. Chambers106A-F contain a sorbent 109A, 109B, 109C, 109D, 109E and 109F,respectively, inlets 110A, 110B, 110C, 110D, 110E and 110F,respectively, for introducing a working fluid or refrigerant 114 intothe chamber for sorption by the sorbent, and outlets 112A, 112B, 112C,112D, 112E and 112F, respectively, for removing the working fluid 114desorbed by the sorbent from the chamber. The working fluid is sorbed ordesorbed from the sorbent in a chamber depending on the temperature andpressure of the sorbent in the chamber. The temperature of the sorbentin each chamber is adjusted by the chamber heating devices 108A, 108B,108C, 108D, 10BE and 108F and the temperature of the heat transferfluid, sometimes referred to herein as the first heat transfer fluid,flowing through the chamber heat conductive passageways 104A-F. Heatingdevices 108A-F can heat compressors 102A-F directly or can heat the heattransfer fluid flowing into heat conductive passageways 104A-F thelatter being preferred. The working fluid used in this example is1,1,1,2-tetrafluoroethane generally referred to as R134a. However, otherworking fluids can be used if desired.

For each of the compressors 102A-F there is a corresponding indirectheat exchanger 120A, 120B, 120C, 120D, 120E and 120F, respectivelyhaving first channels 122A, 122B, 122C, 122D, 122E and 122F,respectively, and second channels 124A, 124B, 124C, 124D, 124E and 124F,respectively, which are hermetically separated from first channels 122.Pump 126, sometimes referred to herein as the first pumping means,conveys the first heat transfer fluid first into channel 122A, then intopassageway 104A, then into channel 122B, then into passageway 104B, theninto channel 122C, then into passageway 104C, then into channel 122D,then into passageway 104D, then into channel 122E, then into passageway104E, then into channel 122F, then into passageway 104F, and then backto pump 126 whereupon the first heat transfer fluid is continuouslyrecycled. As a consequence of the in series connecting of the firstchannels 122 to heat conductive passageways 104 a train 128 of heatconductive passageways 104 is formed having a train inlet 125, which isalso the inlet of first channel 122A, and a train outlet 127, which isalso the outlet of heat conductive passageway 104F. In embodiment 100 itshould be noted that the order of heat conductive passageways 104 andfirst channels 122 always remains the same thereby eliminating the needfor costly control valves in the loop 129 which comprises train 128 andpump 126. This provides a cost saving and increased reliability oversystems requiring additional control valves.

Pump 130, sometimes referred to herein as the second pump means, pumps aheat transfer fluid, sometimes referred to herein as the second heattransfer fluid, through coolant loop 132 which contains six parallelbranches 134A, 134B, 134C, 134D, 134E and 134F containing control valves136A, 136B, 136C, 136D, 136E and 136F, respectively, and second channels124A-F, respectively, of indirect heat exchangers 120A-F, respectively.Valves 136A-F are controlled by controller 140 so that only one ofvalves 136A-F is open at a time thereby permitting the second heattransfer fluid to flow through only one of second channels 124A-F at atime. Before returning to pump 130, the second heat transfer fluid iscooled by radiator 142 to about 38° C. (100° F.) and then continuouslycirculated around coolant loop 132 so that the active second channelalways receives the second heat transfer fluid at a temperature of about38° C. (100° F.). Radiator 142 transfers heat from the second heattransfer fluid to the outside in the summer, and to the room or zone tobe heated in the winter in a conventional manner. In FIG. 1 valve 136Fis open and all the other valves, i.e. valves 136A-E, are closed. FIG. 1represents phase 1 of six phases as will be explained in greater detaillater. In the system of FIG. 1 it is to be noted that only one controlvalve 136 per compressor is required for the second heat transfer fluidof the system, which provides a cost saving advantage to that of systemshaving two or more control valves per compressor.

Heating devices 108A-F, sometimes referred to herein as the primaryheating means, are also controlled by controller 140 so that only one ofthe heating devices is heating at a time for a predetermined period oftime and the remaining heating devices are in active, thereby defining aheating cycle. In the following discussion the temperatures are based onthe use of R134a as the working fluid, and the temperature cycle shownin FIG. 3 which is discussed in greater detail later. In FIG. 1, whichdepicts phase 1, heating device 108C is active and heating the firstheat transfer fluid to a temperature of about 204° C. (400° F.) therebyheating the sorbent in chamber 106° C. to about 204° C. (400° F.).Heating devices 108 add heat to the system at a high temperature, i.e.the heating devices increase the temperature of the first heat transferfluid from about 188° C. (370° F.) to about 204° C. (400° F.). In phase1 the remaining heating devices 106A,B,D-F are not heating theirrespective compressors 102A,B,D-F, respectively. In FIG. 1 the firstheat transfer fluid flowing through the train 128 is also heating thesorbent in chamber 106D and 106E, and at the same time also cooling thesorbent in chambers 106A, 106B and 106F the combination of whichregenerates system heat thereby providing for higher COP's. As mentionedearlier, in FIG. 1 the second heat transfer fluid is flowing through thesecond channel 124F of indirect heat exchangers 120F and thereby coolingthe first heat transfer fluid flowing through the first channel 122F ofindirect heat exchangers 120F. The thusly cooled first heat transferfluid then flows through heat conductive passageway 104F thereby coolingthe sorbent 109F in chamber 106F to a temperature between about 38° C.(100° F.) to about 54° C. (130° F.).

With valve 136F open for cooling the sorbent 109F in chamber 106F, andheating device 108C activated for heating sorbent 106C in chamber 106C,the calculated temperature profiles of the sorbent in chambers 106A-Fare as follows, with the first mentioned temperature corresponding tothe sorbent temperature nearest the inlet of its heat conductivepassageway 104, and the second mentioned temperature corresponding tothe sorbent temperature nearest the outlet of the heat conductivepassageway:

    ______________________________________                                        Compressor      (°C.)                                                                           (°F.)                                         ______________________________________                                        102A             54-129  130-265                                              102B            129-177  265-350                                              102C            204-188  400-370                                              102D            188-104  370-220                                              102E            104-60   220-140                                              102F            38-54    100-130                                              ______________________________________                                    

The above calculated temperature profiles of the first heat transferfluid as it flows through train 128 of compressors is shown in FIG. 2which is a computerized simulation of the system and process. The aboveprofile pertains to a first phase, i.e. phase 1, in the operation of thesystem of embodiment 100. In general the total number of phases will beequal to the number of compressors. For the system of FIG. 1 the numberof phases are six which, when completed, defines a cycle. When a phaseis completed the next phase begins and the temperature profiles in thecompressors shift as follows:

Phase 2, valve 136A open and heating device 108D heating:

    ______________________________________                                        Compresssor     (°C.)                                                                           (°F.)                                         ______________________________________                                        102B             54-129  130-265                                              102C            129-177  265-350                                              102D            204-188  400-370                                              102E            188-104  370-220                                              102F            104-60   220-140                                              102A            38-54    100-130                                              ______________________________________                                    

Phase 3, valve 136B open and heating device 108E heating:

    ______________________________________                                        Compresssor     (°C.)                                                                           (°F.)                                         ______________________________________                                        102C             54-129  130-265                                              102D            129-177  265-350                                              102E            204-188  400-370                                              102F            188-104  370-220                                              102A            104-60   220-140                                              102B            38-54    100-130                                              ______________________________________                                    

Phase 4, valve 136C open and heating device 108F heating:

    ______________________________________                                        Compressor      (°C.)                                                                           (°F.)                                         ______________________________________                                        102D             54-129  130-265                                              102E            129-177  265-350                                              102F            204-188  400-370                                              102A            188-104  370-220                                              102B            104-60   220-140                                              102C            38-54    100-130                                              ______________________________________                                    

Phase 5, valve 136D open and heating device 108A heating:

    ______________________________________                                        Compresssor     (°C.)                                                                           (°F.)                                         ______________________________________                                        102E             54-129  130-265                                              102F            129-177  265-350                                              102A            204-188  400-370                                              102B            188-104  370-220                                              102C            104-60   220-140                                              102D            38-54    100-130                                              ______________________________________                                    

Phase 6, valve 136E open and heat device 108B heating:

    ______________________________________                                        Compressor      (°C.)                                                                           (°F.)                                         ______________________________________                                        102F             54-129  130-265                                              102A            129-177  265-350                                              102B            204-188  400-370                                              102C            188-104  370-220                                              102D            104-60   220-140                                              102E            38-54    100-130                                              ______________________________________                                    

When phase 6 is completed the cycle is completed and a new cycle beginswith phase 1; and, the control valve phases, the heating deviceactivation phases, and the phase temperature profiles repeat as setforth above. The above temperatures are based on the use of R134a as theworking fluid using the cycle shown in FIG. 3. Other working fluids canbe used and the temperatures will vary with the particular working fluidchosen. The working fluid should be chosen with the end use in mind. Forair conditioning of rooms and buildings R134a and R124 are preferredbecause of their useful operating temperature ranges and low ODP_(S).

For longer pump life, it is desirable to maintain a constant lowertemperature at pump 126. This can be achieved by including a radiator144 after the outlet of train 128 for rejecting heat from the first heattransfer fluid to the environment and/or auxiliary heat exchanger 146for exchanging heat between the first heat transfer fluid flowing fromtrain 128 to pump 126 and the first heat transfer fluid flowing frompump 126 to the inlet of train 128. It should be understood thatradiator 144 and auxiliary heat exchanger 146 are optional.

The working fluid or refrigerant side of embodiment 100 containscondenser 150 which provides means for transferring heat from theworking fluid to the environment in the summer or to the room or zone inthe winter, and, means for condensing high temperature, high pressureworking fluid vapor from the compressors to form a low temperature, highpressure working fluid liquid. The working fluid side also containsJoule-Thomson expansion valve 152 which provides means for convertinglow temperature, high pressure working fluid liquid to low temperature,low pressure working fluid liquid and gas, evaporator 154 which providesmeans for converting low temperature, low pressure working fluid liquidto low temperature, low pressure working fluid vapor and for acceptingheat from a low temperature source such as a room or zone in the summerthereby providing comfort cooling, or from the environment in thewinter. Conduits 160 provides means for conveying high temperature, highpressure working fluid vapor from compressors 102 to condenser 150.Conduit 162 provides liquid conveying means for conveying lowtemperature, high pressure working fluid liquid from condenser 150 toJ-T valve 152. Conduit 164 provides liquid conveying means for conveyinglow temperature, low pressure working fluid liquid from J-T valve 152 toevaporator 154. Conduit 166 provides vapor conveying means for conveyinglow temperature, low pressure working fluid vapor from evaporator 154 tocompressors 102.

Conduit 160 contains check valves 170A-F which permit high pressureworking fluid vapor to flow from compressors 102 to condenser 150 whilepreventing high pressure vapor from flowing into compressors 102 whichare under a low pressure. Conduit 166 contains check valves 172A-F whichpermit low pressure working fluid vapor to flow into compressors 102which are under a low pressure while preventing such vapor from flowinginto compressors which are under a higher pressure. In FIG. 1, whichrepresents phase 1 of the cycle, working fluid is being desorbed incompressors 102C-E, and, high temperature, high pressure desorbedworking fluid vapor is flowing through check valves 170C-E to condenser150; while low temperature, low pressure working fluid vapor is flowingfrom evaporator 114 through conduit 166 and check valves 172A,B,F intocompressors 102A,B,F. The high pressure in conduit 160 prevents checkvalves 170A,B,F from opening. The high pressure in compressors 102C-Eprevents check valves 172C-E from opening. Therefore no solenoid controlvalves are required for the working fluid side and consequently thetemperature of the compressors alone determines flow of working fluid toand from the compressors.

To improve the efficiency of embodiment 100, the working fluid side canalso include heat exchanger 174 for exchanging heat between the workingfluid liquid in conduit 162 and the working fluid vapor in conduit 166.

The system of embodiment 100 was evaluated by computer simulation foruse as an air conditioner/heat pump. The computer model was based on anactivated carbon sorbent known as AX-21. AX-21 sorbent was chosenbecause of its extremely high BET surface area which is over 2000 m²/gm. Working fluids or refrigerants chosen for testing were1,1,1,2-tetrafluoroethane known as R134a, and2-chloro-1,1,1,2-tetrafluoroethane known as R124. These working fluidsare preferred because they are believed to be nontoxic, non-flammable,and have high working vapor pressures. Furthermore R134a and R124 have avery low ozone-depletion-potential ("ODP"). The ODP for R134a is 0.0 andfor R124 is less than 0.05 as opposed to an ODP fordichlorodifluoromethane, known as R12, of 1.0. Another useful workingfluid for all embodiments of this invention is dichlorotrifluoroethane,referred to as R123, will also have high COP_(S) while remainingnon-toxic, non-flammable with a low ODP.

The isotherm data for R134a and R124 on AX-21 carbon was measured and isshown in FIGS. 3 and 4, respectively.

R134a/AX-21 Cycle

For the cycle shown in FIG. 3, the adsorption system is heated from 38°C. (100° F.), point A, to 63° C. (146° F.), point B, therebypressurizing the system from a low pressure or P_(L) of 335 kpa (48.5psia) to a high pressure or P_(H) of 964 kpa (139.7 psia). When heatedan additional amount from 63° C. (146° F.), point B, to 204° C. (400°F.), point D, R134a is desorbed from the carbon sorbent at a constanthigh pressure of 964 kpa (139.7 psia). During cooling from 204° C. (400°F.), point D, to 162° C. (324° F.), point E, the system pressure isreduced without adsorbing significant amounts of R134a. When the systemis further cooled from 162° C. (324° F.), point E, to 38° C. (100° F.),point A, R134a is adsorbed at a constant low pressure of 335 kpa (48.5psia). In this example the pressure ratio, or P_(H) /P_(L), of the cycleis about 2.9.

At high pressure, specifically 964 kpa (139.7 psia), R134a vapor iscondensed at 38° C. (100° F.) thereby rejecting heat to a relatively lowtemperature heat sink, 38° C. (100° F.), such as the environment in thesummer and the room interiors in the winter, or to a hot water systemfor tap water heating year around. When R134a is expanded to 335 kpa(48.5 psia), it cools to 4° C. (40° F.) thereby providing a 4° C. (40°F.) heat sink useful for cooling room interiors in summer or a heat sinkfor the acceptance of low temperature heat from the environment duringthe winter.

Because the embodiments of this invention are capable of regenerating upto about 99% of the sensible heat, the primary net heat required is thatportion of the cycle where the thermal capacitance of the system, i.e.BTU/°F., is higher during heat-up than during cool-down. The thermalcapacitance for FIG. 3 is high during heat-up 57° C. (134° F.) to 204°C. (400° F.) due to the added heat of desorption. The thermalcapacitance for FIG. 3 is also high during cool-down 162° C. (324° F.)to 38° C. (100° F.) due to the added heat of adsorption. Therefore theonly region where the heating thermal capacitance is significantlyhigher than the cooling thermal capacitance is during heating from 162°C. (324° F.), point C, to 204° C. (400° F.), point D; and the amount ofR134a removed during such heating is about 0.694-0.482, or 0.212 gram ofR134a per gram of carbon sorbent.

The heat of adsorption of R134a on AX-21 carbon sorbent has beenmeasured and found to be about 9.5 Kcal/mole. The heat of refrigerationof R134a is known to be 4.7 kcal/mole. The total mass of R134a desorbedfor the cycle shown in FIG. 3 is 1.187-0.482, or 0.705 grams of R134aper gram of AX-21 carbon sorbent. Therefore the total COP for cooling,or COP_(C), can be as high as about (0.705×4.7)/(0.212×9.5), or about1.65 for pumping heat from 4° C. (40° F.) at R134a to 38° C. (100° F.).That is for every watt of heat added at about 204° C. (400° F.), 1.65watts can be ideally removed at 4° C. (40° F.). Since the 204° C. (400°F.) heat and the 4° C. (40° F.) heat are both removed from the system at38° C. (100° F.), the total COP for heating, or COP_(H), can be as highas about 1.65+1.0, or about 2.65. Based on the above, the fraction ofthe heat of adsorption which is regenerated is (0.705-0.212)/0.705 orabout 0.70, i.e. about 70% of the heat of adsorption is regenerated.

R124/AX-21 Cycle

For the cycle shown in FIG. 4, the adsorption system is heated from 38°C. (100° F.), point A, to 58° C. (137° F.), point B, therebypressurizing the system from a low pressure or P_(L) of 153 kpa (22.2psia) to a high pressure or P_(H) of 434 kpa (62.9 psia). When heated anadditional amount from 58° C. (137° F.), point B, to 204° C. (400° F.),point D, R124 is desorbed from the carbon sorbent at a constant highpressure of 434 kpa (62.9 psia). During cooling from 204° C. (400° F.),point D, to 168° C. (334° F.), point E, the system pressure is reducedwithout adsorbing significant amounts of R124. When the system isfurther cooled from 168° C. (334° F.), point E, to 38° C. (100° F.),point A, R124 is adsorbed at a constant low pressure of 153 kpa (22.2psia). In this example the pressure ratio, or P_(H) /P_(L), of the cycleis about 2.8.

At high pressure, specifically 434 kpa (62.9 psia), R124 vapor iscondensed at 38° C. (100° F.) thereby rejecting heat to a relatively lowtemperature heat sink, 38° C. (100° F.), such as the environment in thesummer and the room interiors in the winter, or to a hot water systemfor tap water heating year around. When R124 is expanded to 153 kpa(22.2 psia), it cools to 4° C. (40° F.) thereby providing a 4° C. (40°F.) heat sink useful for cooling room interiors in summer or a heat sinkfor the acceptance of low temperature heat from the environment duringthe winter.

Because the embodiments of this invention are capable of regenerating upto about 99% of the sensible heat, the primary net heat required is thatportion of the cycle where the thermal capacitance of the system, i.e.BTU/°F., is higher duping heat-up than during cool-down. The thermalcapacitance for FIG. 4 is high during heat-up 58° C. (137° F.) to 204°C. (400° F.) due to the added heat of desorption. The thermalcapacitance for FIG. 4 is also high during cool-down 168° C. (334° F.)to 38° C. (100° F.) due to the added heat of adsorption. Therefore theonly region where the heating thermal capacitance is significantlyhigher than the cooling thermal capacitance is during heating from 168°C. (334° F.), point C, to 204° C. (400° F.), point D; and the amount ofR124 removed during such heating is about 0.752-0.550, or 0.202 gram ofR124 per gram of carbon sorbent.

The heat of adsorption of R124 on AX-21 carbon sorbent has been measuredand found to be about 10.7 Kcal/mole. The heat of refrigeration of R124is known to be 4.4 kcal/mole. The total mass of R124 desorbed for thecycle shown in FIG. 4 is 1.352-0.550, or 0.802 grams of R124 per gram ofAX-21 carbon sorbent. Therefore the total COP for cooling, or COP_(C),can be as high as about (0.802×4.4)/(0.202×10.7), or about 1.63 forpumping heat from 4° C. (40° F.) at R124 to 38° C. (100° F.). That isfor every watt of heat added at about 204° C. (400° F.), 1.63 wants canbe ideally removed at 4° C. (40° F.). Since the 204° C. (400° F.) heatand the 4° C. (40° F.) heat are both removed from the system at 38° C.(100° F.), the total COP for heating, or COP_(H), can be as high asabout 1.63+1.0, or about 2.63. Based on the above, the fraction of theheat of adsorption which is regenerated is (0.802-0.202)/0.802 or about0.75, i.e. about 75% of of the heat of adsorption is regenerated.

FIG. 5 is a second embodiment of this invention generally designated bynumeral 200 in which the primary heating means 108 comprises secondindirect heat exchangers 202A-F having first channels 204A-F for thefirst heat transfer fluid and second channels 206A-F for another heattransfer fluid, sometimes referred to herein as the third heat transferfluid. First channels 204A-F are also seen to be included in train 128.Heating means 108 also comprises pump 210, sometimes referred to hereinas the third pump means, for pumping the third heat transfer fluidthrough heating loop 212 which contains six parallel branches 214A,214B, 214C, 214D, 214E and 214F containing control valves 216A, 216B,216C, 216D, 216E and 216F, respectively, and second channels 206A-F,respectively, of indirect heat exchangers 202A-F, respectively. Controlvalves 216A-F are sometimes referred to herein as the second controlvalves. Before returning to pump 210, the third heat transfer fluid isheated by healer 220 to about 204° C. (400° F.) and then continuouslycirculated around heating loop 212 so that the active second channel 206always receives the third heat transfer fluid at a temperature of about204° C. (400° F.).

Control valves 21GA-F are also controlled by controller 140 so that onlyone of the valves 216A-F is open at a time for a predetermined period oftime and the remaining valves are closed, thereby defining a heatingcycle. In FIG. 5, which depicts phase 1 of six phases, valve 216C isopen thereby permitting heat to be transferred from the third heattransfer fluid in second channel 206C to the first heat transfer fluidin first channel 204C so that it too is heated to a temperature of about204° C. (400° F.) and which thereby heats the sorbent in chamber 106Calso to about 204° C. (400° F.). In phase 1 the remaining valves216A,B,D-F are closed thereby preventing heating of the first heattransfer fluid in first channels 204A,B,D-F by the circulating thirdheat transfer fluid in heating loop 212. The phases and temperatures ofembodiment 200 are the same as those described above for embodiment 100shown in FIG. 1.

FIG. 6 is a third embodiment of this invention, generally designated bynumeral 230, having four compressors 102A, 102B, 102C and 102D and asingle pump 232 which conveys a first heat transfer fluid through boththe cooling loop 234 and the train 238 of heat conductive passageways104A, 104B, 104C and 104D. Train 238 has train inlet 125 and trainoutlet 239 which is also the outlet of heat conductive passageway 104D.The primary heating means 108A, 108B, 108C and 108D has been generallyindicated as in FIG. 1. Means 108 can be similar to that described forembodiments 100 and 200 or any other suitable method of adding heatduring a heating cycle to the compressors. This embodiment has fourphases because there are four compressors. It should be understood,however, that systems with six compressors are preferred to systems withfour because more heat is regenerated. FIG. 6 depicts the first phase inwhich heating device 108B is active and control valve 136D is open whileheating devices 108A, 108C and 108D are inactive and valves 136A, 136Band 136C are closed. In this embodiment expected temperature in thephases are as follows:

    ______________________________________                                        Compressor      (°C.)                                                                           (°F.)                                         ______________________________________                                        102A             66-166  150-330                                              102B            204-177  400-350                                              102C            177-71   350-160                                              102D            38-66    100-150                                              ______________________________________                                    

The above calculated temperature profiles of the first heat transferfluid as it flows through train 128 of compressors is shown in FIG. 9which is a computerized simulation of the system and process. The aboveprofile pertains to a first phase, i.e. phase 1, in the operation of thesystem of embodiment 100. In general the total number of phases will beequal to the number of compressors. For the system of FIG. 1 the numberof phases are six which, when completed, defines a cycle. When a phaseis completed the next phase begins and the temperature profiles in thecompressors shift as follows:

Phase 2, valve 136A open and heating device 108C heating:

    ______________________________________                                        Compresssor     (°C.)                                                                           (°F.)                                         ______________________________________                                        102B             66-166  150-330                                              102C            204-177  400-350                                              102D            177-71   350-160                                              102A            38-66    100-150                                              ______________________________________                                    

Phase 3, valve 136B open and heating device 108D heating:

    ______________________________________                                        Compresssor     (°C.)                                                                           (°F.)                                         ______________________________________                                        102C             66-166  150-330                                              102D            204-177  400-350                                              102A            177-71   350-160                                              102B            38-66    100-150                                              ______________________________________                                    

Phase 4, valve 136C open and heating device 108A heating:

    ______________________________________                                        Compresssor     (°C.)                                                                           (°F.)                                         ______________________________________                                        102D             66-166  150-330                                              102A            204-177  400-350                                              102B            177-71   350-160                                              102C            38-66    100-150                                              ______________________________________                                    

When phase 4 is completed the cycle is completed and a new cycle beginswith phase 1; and, the control valve phases, the heating deviceactivation phases, and the phase temperature profiles repeat as setforth above.

FIG. 7 is a fourth embodiment of this invention generally designated bynumeral 240 having four compressors 102A, 102B, 102C and 102D and asingle pump 242 which conveys a first portion of first heat transferfluid through the cooling loop 244 and a second portion of the firstheat transfer fluid through the train 246 of heat conductive passageways104. Train 246 has train inlet 125 and train outlet 247 which is alsothe outlet of heat conductive passageway 104D. Although this embodimentis also depicted with four compressors it should be understood thatsystems with six compressors are preferred to systems with four becausemore heat is regenerated. The primary heating means, i.e. elements 108A,108B, 108C and 108D, is generally indicated as in FIG. 1. Means 108 canbe similar to that described for embodiments 100 and 200, or any othersuitable method of adding heat during a heating cycle to thecompressors. Since this embodiment has four phases there are fourcompressors. FIG. 7 depicts the first phase of four phases in whichheating device 108B is active and control valve 136D is open whileheating devices 108A, 108C and 108D are inactive and valves 136A, 136Band 136C are closed. In this embodiment expected temperatures in thefour phases are the same as those set forth above for embodiment 230.When phase 4 is completed the cycle is completed and a new cycle beginswith phase 1; and, the control valve phases, the heating deviceactivation phases, and the phase temperature profiles repeat as setforth above with regard to embodiment 230.

In embodiment 240 the working fluid or refrigerant side has a separateworking fluid loop for each compressor rather than one evaporator 114 asin the previously discussed embodiments. For example, the working fluidis desorbed from compressor 102A at a high pressure is permitted bycheck valve 170A to flow into conduit 160A to radiator or condenser 150Awhereupon heat is discharged to the environment. The working fluid isthen expanded through J-T valve 150A and then introduced into evaporator154A whereupon liquid is collected. At the point in the heating cyclewhen the pressure in compressor 102A is lowered sufficiently, theworking fluid is evaporated in evaporator 114A and the vapor ispermitted by check valve 172A to enter into compressor 102A through line166A. As depicted in FIG. 7, each compressor has its own working fluidcondenser, J-T valve and evaporator which function in the same manner asdescribed for compressor 102A. It should be understood, however, thatthe working fluid or refrigerant side can be as in shown in FIGS. 1 and6 rather than as shown in FIG. 7 depending on the particular intendeduse of the system.

FIG. 8 is a fifth embodiment of this invention generally designated bynumeral 250 having four compressors 102A, 102B, 102C and 102D and asingle pump 252 which conveys a first heat transfer fluid through boththe cooling loop and the train of heat conductive passageways 104A,104B, 104C and 104D. In this embodiment it is to be noted that indirectheat exchangers 120, as employed in the embodiment of FIG. 7, are notrequired. The primary heating means 108A, 108B, 108C and 108D has beengenerally indicated as in FIG. 1. Means 108 can be similar to thatdescribed for embodiments 100 and 200 or any other suitable method ofadding heat during a heating cycle to the compressors. This embodimenthas four phases because there are four compressors. It should beunderstood, however, that systems with six compressors are preferred tosystems with four because more heat is regenerated. FIG. 8 depicts thefirst phase in which heating device 108B is active and control valve136D is open while heating devices 108A, 108C and 108D are inactive andvalves 136A, 136B and 136C are closed. In this embodiment there is asecond set of control valves 254A, 254B, 254C and 254D and acorresponding set of check valves 256A, 256B, 256C and 256D. Thereforethe train of heat conductive passageways 104A-D also includes valves136A-D, valves 254A-D and valves 256A-D.

In phase 1 heating device 108B is activated and heating the sorbent inchamber 109B. Simultaneously with such heating, the first heat transferfluid after being cooled in radiator 142, is conveyed by pump 252 tocontrol valve 136D which is open; valves 136A-C being closed. The cooledfirst heat transfer fluid then enters heat conductive passageway 104D.Since valve 254D is closed, the line pressure forces check valve 256Dopen so that the heat transfer fluid then enters heat conductivepassageway 104A. Since valve 254A is closed, the line pressure forcescheck valve 256A open so that the heat transfer fluid then enters heatconductive passageway 104B. Since valve 254B is closed, the linepressure forces check valve 256B open so that the heat transfer fluidthen enters heat conductive passageway 104C. Since valve 254C is open,the higher line pressure in conduit 258 prevents check valve 256C fromopening so that the heat transfer fluid then flows through valve 254Cand back to radiator 142. Valves 136A-D and 254A-D and primary heatingmeans 108A-D are all controlled by controller 140 so that apredetermined valve from set 136 and 254 will remain open apredetermined period of time which corresponds to the heating cycle of apredetermined activated heating device 108. In this embodiment the firstheat conductive passageway in the train of heat conductive passagewaysvaries depending upon which one of the four phases of the cycle isactive. In phase 1, working fluid is being desorbed in chambers 109B and109C, and adsorbed in chambers 109D and 109A.

In embodiment 250 the expected temperatures in the four phases are thesame as those set Forth above for embodiment 230. When phase 4 iscompleted the cycle is completed and a new cycle begins with phase 1;and, the control valve phases, the heating device activation phases, andthe phase temperature profiles repeat as set forth above with regard toembodiment 230. These expected temperatures are without "topping" or"bottoming" after each phase. Topping and/or bottoming after each phasecan improve performance even more. For example, at the end of phase 1,an optional topping or bottoming step may be added to further reducethermal gradients in the hottest or coolest compressor. To provide"bottoming", i.e. to cool compressor 102D further, valves 136D and 254Dwould be open for a predetermined period of time, while all other valvesare closed. To provide "topping" at the end of Phase 1, heating means108D would be activated while the series flow of heat transfer fluidthrough all the compressors is interrupted, or while "bottoming" istaking place.

In embodiment 250 the working fluid or refrigerant side has not beenshown since it can be as in shown in FIGS. 1 and 6 or as shown in FIG. 8depending on the particular intended use of the system.

In all of the above described examples the temperature profiles in theseveral compressors were based on the use of R134a as the working fluidand the cycle shown in FIG. 3. Other working fluids can be used.

Examples of useful heat transfer fluids are the Dowtherm™ brand fluidsand water. Other heat transfer fluids can also be used if desired.

In general, for all embodiments, it should be noted that by keeping thepressure ratio P_(H) /P_(L) close to unity, it is possible to regeneratealmost all of both the sensible heat and the heat of adsorption. That issystems which have P_(H) /P_(L) very close to unity will take verylittle power to operate.

It should be noted that by keeping the pressure ratio or P_(H) /P_(L)low and the temperature overlap of the sorbing and desorbing operationshigh that it is possible to regenerate at least some of the heat ofadsorption. Therefore in one embodiment of this invention the P_(H)/P_(L) is no greater than about 3 and the temperature overlap is atleast about 77 Celsius (170 Fahrenheit) degrees.

Detailed computerized thermal models have shown that the final COP_(S)for the embodiments of this invention can be at least about 90% of theideal COP_(S). The improved results of this invention are due primarilyto the low thermal gradients in the compressors achieved through theimproved regenerative heat systems of this invention, whereas the largethermal gradients existing in the prior art systems cause inherent largesystem energy losses. The elimination of such thermal gradients allows amuch higher regeneration efficiency for the system.

In all systems, however, there are minor losses due to parasitic heatloss from insulated surfaces, small regenerator inefficiencies,circulation pump power requirements, end-to-end sorption canisterconduction heat leaks, and hot exhausting refrigerant gas thermalcapacitance heat loss. These losses can be minimized by conventionalheat design techniques of external insulation, low coolant line pressuredrop passages, low end-to-end sorption canister thermal conductancedesign, and refrigerant vapor thermal regenerators.

While the preferred embodiments of the present invention have beendescribed, it should be understood that various changes, adaptations andmodifications may be made thereto without departing from the spirit ofthe invention and the scope of the appended claims. It should beunderstood, therefore, that the invention is not to be limited to minordetails of the illustrated invention shown in preferred embodiment andthe figures and that variations in such minor details will be apparentto one skilled in the art.

Therefore it is to be understood that the present disclosure andembodiments of this invention described herein are for purposes ofillustration and example and that modifications and improvements may bemade thereto without departing from the spirit of the invention or fromthe scope of the claims. For example, conventional flow systemscomponents such as accumulators and additional pumps and the like can beincluded in the systems if desired. The claims, therefore, are to beaccorded a range of equivalents commensurate in scope with the advancesmade over the art.

INDUSTRIAL APPLICABILITY

The regenerative adsorbent heat pump processes and systems of thisinvention are useful for air conditioning rooms and buildings and canalso be used for heating in the winter and producing hot waterthroughout the year, and in general, for pumping heat from a lowtemperature to a higher temperature.

I claim:
 1. A regenerative sorbent heat pump process for cooling aninterior space and for simultaneously regenerating at least a portion ofthe heat of adsorption comprising:(a) confining a sorbent in a pluralityof compressor zones, the number of compressor zones being at least four;(b) introducing a working fluid vapor from an evaporization zone into atleast one of the number of compressor zones and sorbing the workingfluid vapor on the sorbent therein over a predetermined firsttemperature range and a predetermined first pressure or P_(L) ; (c)desorbing working fluid vapor from the sorbent in at least one of theremaining number of compressor zones and removing working fluid vaportherefrom over a predetermined second temperature range which is higherthan the predetermined first temperature range and at a predeterminedsecond pressure or P_(H) which is larger than the predetermined firstpressure, a part of the predetermined first temperature rangeoverlapping a part of the predetermined second temperature range; (d)condensing working fluid vapor removed from said at least one of theremaining number of the compressor zones at P_(H) and transferring heatfrom the working fluid to the environment thereby forming a workingfluid liquid; (e) evaporating the working fluid liquid and forming theworking fluid vapor in the evaporation zone at P_(L) by transferringheat from an interior space to the evaporation zone thereby cooling theinterior space; (f) circulating a heat transfer fluid in a closed loopwhich comprises a heat removal zone and series flow through thecompressor zones and preventing the heat transfer fluid from directlycontacting the sorbent; (g) removing heat from the heat transfer fluidin the heat removal zone and transferring it to the environment; (h)adding heat from a heat source to a predetermined one of the compressorzones over a predetermined period of time; (i) cooling the coolestcompressor further to a predetermined bottoming temperature; (j) afterstep (i), repeating step (h) sequentially in each of the compressorzones; (k) indirectly transferring heat from the sorbent in thecompressor zones which are sorbing working fluid vapor to the heattransfer fluid and from the heat transfer fluid to the sorbent in thecompressor zones which are desorbing working fluid vapor therebyregenerating heat; and, (l) maintaining the P_(H) /P_(L) ratiosufficiently low so that at least a portion of the heat of absorption isregenerated.
 2. The process of claim 1, further comprising maintainingthe P_(H) /P_(L) ratio between about 1.1 and about
 10. 3. The process ofclaim 1, further comprising maintaining the P_(H) /P_(L) ratio betweenabout 1.1 and about
 5. 4. The process of claim 1, further comprisingmaintaining the P_(H) /P_(L) ratio between about 1.1 and about
 3. 5. Theprocess of claim 1, further comprising maintaining the P_(H) /P_(L)ratio sufficiently Low that about 25% of the heat of adsorption isregenerated.
 6. The process of claim 1, further comprising maintainingthe P_(H) /P_(L) ratio sufficiently low that about 50% of the heat ofadsorption is regenerated.
 7. The process of claim 1, further comprisingmaintaining the P_(H) /P_(L) ratio sufficiently low that about 70% ofthe heat of adsorption is regenerated.
 8. The process of claim 1,wherein the predetermined first temperature range is from at least about-18° C. to no more than about 204° C., wherein the predetermined secondtemperature range is from at Least about 38° C. to no more than about427° C., and, wherein the predetermined first and predetermined secondtemperature ranges overlap at least about 28 Celsius degrees.
 9. Theprocess of claim 1, wherein the predetermined first temperature range isfrom at least about -18° C. to no more than about 204° C., wherein thepredetermined second temperature range is from at least about 32° C. tono more than about 316° C., and, wherein the predetermined first andpredetermined second temperature ranges overlap at least about 56Celsius degrees.
 10. The process of claim 1, wherein the predeterminedfirst temperature range is From at least about -18° C. to no more thanabout 204° C., wherein the predetermined second temperature range isfrom at Least about 38° C. to no more than about 260° C., and, whereinthe predetermined first and predetermined second temperature rangesoverlap at least about 56 Celsius degrees.
 11. The process of claim 1,wherein the predetermined first temperature range is from at least about10° C. to no more than about 177° C., wherein the predetermined secondtemperature range is from at least about 38° C. to no more than about232° C., and, wherein the predetermined first and predetermined secondtemperature ranges overlap at least about 83 Celsius degrees.
 12. Theprocess of claim 1, wherein the working fluid is selected from the groupconsisting of fluorine substituted ethanes, and, fluorine and chlorinesubstituted ethanes.
 13. The process of claim 1, wherein the workingfluid is selected from the group consisting of2-chloro-1,1,1,2-tetrafluoroethane, 1,1-dichloro-2,2,2-trifluoroethane,1,1,1,2-tetrafluoroethane, ammonia, and water.
 14. The process of claim1, wherein the sorbent selected from the group consisting of activatedcarbons, zoolites, silica gels and alumina.
 15. A regenerative sorbentheat pump process for cooling an interior space and for simultaneouslyregenerating at least a portion of the heat of adsorption comprising:(a)confining a sorbent in a plurality of compressor zones, the number ofcompressor zones being at least four; (b) introducing a working fluidvapor from an evaporation zone into at least one of the number ofcompressor zones and sorbing the working fluid vapor on the sorbenttherein over a predetermined first temperature range and a predeterminedfirst pressure or P_(L) ; (c) desorbing working fluid vapor from thesorbent in at least one of the remaining number of compressor zones andremoving working fluid vapor therefrom over a predetermined secondtemperature range which is higher than the predetermined firsttemperature range and at a predetermined second pressure or P_(H) whichis higher than the predetermined first pressure, a part of thepredetermined first temperature range overlapping a part of thepredetermined second temperature range; (d) condensing working fluidvapor removed from said at least one of the remaining number of thecompressor zones at P_(H) and transferring heat from the working fluidto the environment thereby forming a working fluid liquid; (e)evaporating the working fluid liquid and forming the working fluid vaporin the evaporation zone at P_(L) by transferring heat from an interiorspace to the evaporation zone thereby cooling the interior space; (f)circulating a heat transfer fluid in a closed loop which comprises aheat removal zone and series flow through the compressor zones andpreventing the heat transfer fluid from directly contacting the sorbent;(g) removing heat from the heat transfer fluid in the heat removal zonebefore it flows to a predetermined one of the compressor zones andtransferring the removed heat to the environment; (h) cooling thecoolest compressor further to a predetermined bottoming temperature; (i)after step (h), repeating step (g) sequentially for each of thecompressor zones; (j) adding heat from a heat source to a predeterminedone of the compressor zones over a predetermined period of time; (k)repeating step (j) sequentially in each of the compressor zones; (l)indirectly transferring heat from the sorbent in the compressor zoneswhich are sorbing working fluid vapor to the heat transfer fluid andfrom the heat transfer fluid to the sorbent in the compressor zoneswhich are desorbing working fluid vapor thereby regenerating heat; and,(m) maintaining the P_(H) /P_(L) ratio sufficiently low so that at leasta portion of the heat of adsorption is regenerated.
 16. A regenerativesorbent heat pump process for cooling an interior space and forsimultaneously regenerating at least a portion of the heat of adsorptioncomprising:(a) confining a sorbent in a plurality of compressor zones,the number of compressor zones being at least four; (b) introducing aworking fluid vapor from an evaporation zone into at least one of thenumber of compressor zones and sorbing the working fluid vapor on thesorbent therein over a predetermined first temperature range and apredetermined first pressure or P_(L) ; (c) desorbing working fluidvapor from the sorbent in at least one of the remaining number ofcompressor zones and removing working fluid vapor therefrom over apredetermined second temperature range which is higher than thepredetermined first temperature range and at a predetermined secondpressure or P_(H) which is higher than the predetermined first pressure,a part of the predetermined first temperature range overlapping a partof the predetermined second temperature range; (d) condensing workingfluid vapor removed from said at least one of the remaining number ofthe compressor zones at P_(H) and transferring heat from the workingfluid to the environment thereby forming a working fluid liquid; (e)evaporating the working fluid liquid and forming the working fluid vaporin the evaporation zone at P_(L) by transferring heat from an interiorspace to the evaporation zone thereby cooling the interior space; (f)circulating a first heat transfer fluid in a closed loop which comprisesa heat removal zone and series flow through the compressor zones andpreventing the first heat transfer fluid from directly contacting thesorbent; (g) indirectly transferring heat from the first heat transferfluid in the heat removal zone before it flows to a predetermined one ofthe compressor zones to a second heat transfer fluid; (h) removing heatfrom a second heat transfer fluid and transferring it to theenvironment; (i) adding heat from a heat source to a predetermined oneof the compressor zones over a predetermined period of time; (j) coolingthe coolest compressor further to a predetermined bottoming temperature;(k) after step (j), repeating step (i) sequentially in each of thecompressor zones; (l) indirectly transferring heat from the sorbent inthe compressor zones which are sorbing working fluid vapor to the firstheat transfer fluid and from the first heat transfer fluid to thesorbent in the compressor zones which are desorbing working fluid vaporthereby regenerating heat; and, (m) maintaining the P_(H) /P_(L) ratiosufficiently low so that at least a portion of the heat of adsorption isregenerated.
 17. The process of claim 16, further comprising repeatingstep (g) sequentially for each of the compressor zones.
 18. The processof claim 16, wherein adding heat from a heat source to a predeterminedone of the compressor zones over a predetermined period of time isperformed by adding heat to a third heat transfer fluid, and, indirectlytransferring heat from the third heat transfer fluid to the first heattransfer fluid before it enters the predetermined one of the compressorzones.
 19. The process of claim 18, further comprising repeating step(g) sequentially for each of the compressor zones.
 20. A regenerativesorbent heat pump system comprising:a working fluid being operable forbeing sorbed by a sorbent; a plurality of compressors, the number ofcompressors being at least four, each of the compressors havinga sorbentcontained within the compressor, and a heat conductive passageway havingan inlet and an outlet, the heat conductive passageway for flowing aheat transfer fluid through the compressor and for indirectlytransferring heat between the sorbent and the heat transfer fluidwithout the heat transfer fluid being in contact with the sorbent; meansfor removing high temperature, high pressure working fluid vapor fromeach of the compressors; condensing means for transferring heat from theworking fluid to a low temperature heat sink, and, for condensingworking fluid vapor to form a low temperature, high pressure workingfluid liquid; evaporating means for converting low temperature, highpressure working fluid liquid to low temperature, low pressure workingfluid vapor, and, for transferring heat from a low temperature sourceexternal of the system to the working fluid; liquid conveying means forconveying low temperature, high pressure working fluid liquid from thecondensing means to the evaporating means; vapor conveying means forconveying low temperature, low pressure working fluid vapor into each ofthe compressors; a first heat transfer fluid and a second heat transferfluid; a plurality of indirect heat exchange means, the number ofindirect heat exchange means being equal to the number of thecompressors, each of the indirect heat exchange means having a firstchannel for flowing the first heat transfer fluid, and a second channelfor flowing the second heat transfer fluid, the channels being isolatedfrom fluid communication with each other, the first channel being inheat conductive communication with the second channel, each of thechannels having an inlet and an outlet; a train formed by connecting inalternating order, the first channels of the indirect heat exchangemeans to the heat conductive passageways, the train having an inletwhich is also the inlet of the first channel of the first-in-the-seriesof indirect heat exchange means of the train, and, the train having anoutlet which is also the outlet of the heat conductive passageway of thelast-in-the-series of compressors of the train; first pumping means forpumping the first heat transfer fluid around the train, the outlet ofthe first pumping means being connected to the train inlet and the trainoutlet being connected to the first pumping means inlet; second pumpingmeans for pumping the second heat transfer fluid; connecting means forconnecting the outlet of the second pumping means to the inlet of thesecond channel of each of the internal heat exchange means, and forconnecting the outlet of each of the second channels thereof to thesecond pumping means inlet; flow control mean for directing the secondheat transfer fluid from the second pumping means to the second channelof a predetermined one of the indirect heat exchange means in apredetermined order thereby defining a flow cycle, and, for enablingheat transfer between the first heat transfer fluid in the first channelthereof and the second heat transfer fluid in the second channelthereof; primary heating means for heating each of the compressors; heatcontrol means for controlling the heating period of the primary heatingmeans in each of the compressors thereby defining a heating cycle; and,heat discharge means for transferring heat from the second heat transferfluid in the connecting means from the second channels to the secondpump means, to a low temperature heat sink thereby providing aregenerative sorbent heat pump system.
 21. The system of claim 20,wherein the number of compressors is four.
 22. The system of claim 20,wherein the number of compressors is six.
 23. The system of claim 20,further comprising heat exchanger means for the indirect transfer ofheat between the low temperature, high pressure working fluid liquid inthe liquid conveying means and the low temperature, low pressure workingfluid vapor in the vapor conveying means.
 24. The system of claim 20,further comprising means for coordinating the flow cycle and the heatingcycle.
 25. The system of claim 20, further comprising auxiliary heatexchanger means for indirectly exchanging heat between the first heattransfer fluid flowing to the train and the first heat transfer fluidflowing from the train.
 26. The system of claim 20, further comprisingmeans for transferring heat from the first heat transfer fluid flowingfrom the train to a low temperature heat sink.
 27. The system of claim25, further comprising means for transferring heat from the first heattransfer fluid flowing from the auxiliary heat exchanger means to a lowtemperature heat sink.
 28. The system of claim 20, wherein the workingfluid is sorbed over a predetermined first temperature range from atleast about -18° C. to no more than about 204° C. wherein the workingfluid is desorbed over a predetermined second temperature range from atleast about 38° C. to no more than about 427° C., and, wherein thepredetermined. First and predetermined second temperature ranges overlapat least about 28 Celsius degrees.
 29. The system of claim 20, whereinthe working fluid selected From the group consisting of fluorinesubstituted ethanes, fluorine and chlorine substituted ethanes, and,wherein the sorbent is selected From the group consisting activatedcarbons.
 30. The system of claim 20, wherein the primary heating meanscomprises a heating device between each of the compressors in the trainand between the first pumping means outlet and the inlet to the heatconductive passageway of each compressor, the heating devices forheating the first heat transfer fluid before it is introduced into thecompressor for which it is intended, the thusly heated first heattransfer fluid thereby heating said compressor.
 31. The system of claim20, further comprising a plurality of second indirect heat exchangemeans, the number of second indirect heat exchange means being equal tothe number of the compressors, each of the second indirect heat exchangemeans having a first channel for flowing a heat transfer fluid, and asecond channel for flowing a heat transfer fluid, the channels thereofbeing isolated from communication with each other, the first channelthereof being in heat conductive communication with the second channelthereof, each of the channels thereof having an inlet and anoutlet;wherein the train includes the first channels of the secondindirect heat exchange means connected, relative to the heat conductivepassageways, in alternating order before each of the heat conductivepassageways; and, further comprising third pumping means for pumping athird heat transfer fluid; second connecting means for connecting theoutlet of the third pumping means to the inlet of the second channel ofeach of the second internal heat exchange means, and for connecting theoutlet of each of the second channels thereof to the third pumping meansinlet; and, flow control means for directing the third heat transferfluid from the third pumping means to the second channel of apredetermined one of the second indirect heat exchange means in apredetermined order thereby defining a second flow cycle, and, forenabling heat transfer between the first heat transfer fluid in thefirst channel thereof and the third heat transfer fluid in the secondchannel thereof; and, wherein the primary heating means includes aheating device in the second connecting means for heating the third heattransfer fluid before it is introduced into the second channel of apredetermined one of the second indirect heat exchange means; and,wherein the heat control means includes means for controlling thetemperature of the third heat transfer fluid heated by the heatingdevices.
 32. A regenerative sorbent heat pump system comprising:aworking fluid being operable for being sorbed by a sorbent; a pluralityof compressors, the number of compressors being at least four, each ofthe compressors havinga sorbent contained within the compressor, and aheat conductive passageway having an inlet and an outlet, the heatconductive passageway for flowing transfer fluid through the compressorand for indirectly transferring heat between the sorbent and the heattransfer fluid without the heat transfer fluid being in contact with thesorbent; means for removing high temperature, high pressure workingfluid vapor from each of the compressors; condensing means fortransferring heat from the working fluid to a low temperature heat sink,and, for condensing working fluid vapor to form a low temperature, highpressure working fluid liquid; evaporating means for converting lowtemperature, high pressure working fluid liquid to low temperature, lowpressure working fluid vapor, and, for transferring heat from a lowtemperature source external of the system to the working fluid; liquidconveying means for conveying low temperature, high pressure workingfluid liquid from the condensing means to the evaporating means; vaporconveying means for conveying low temperature, low pressure workingfluid vapor into each of the compressors; a heat transfer fluid; aplurality of indirect heat exchange means, the number of indirect heatexchange means being equal to the number of the compressors, each of theindirect heat exchange means having a first channel for flowing the heattransfer fluid, and a second channel for flowing the heat transferfluid, the channels being isolated from immediate fluid communicationwith each other, the first channel being in heat conductivecommunication with the second channel, each of the channels having aninlet and an outlet; a train formed by connecting in alternating order,the first channels of the indirect heat exchange means to the heatconductive passageways, the train having an inlet which is also theinlet of the first channel of the first-in-the-series of the indirectheat exchange means of the train, and, the train having an outlet whichis also the outlet of the heat conductive passageway of thelast-in-the-series of compressors of the train; pumping means forpumping the heat transfer fluid; first connecting means for connectingthe outlet of the pumping means to the inlet of each of the secondchannels; second connecting means for connecting the outlet of each ofthe second channels to the train inlet; third connecting means forconnecting the train outlet to the pumping means inlet; flow controlmeans for directing the heat transfer fluid from the pumping means tothe second channel of a predetermined one of the indirect heat exchangemeans in a predetermined order thereby defining a flow cycle, and, forenabling heat transfer between the heat transfer fluid in the firstchannel thereof and the heat transfer fluid in the second channelthereof; primary heating means for heating each of the compressors; heatcontrol means for controlling the heating period of the primary heatingmeans in each of the compressors thereby defining a heating cycle; and,heat discharge means for transferring heat from the heat transfer fluidin the second connecting means to a low temperature heat sink therebyproviding a regenerative sorbent heat pump system.
 33. The system ofclaim 32, further comprising auxiliary heat exchanger means forindirectly exchanging heat between the heat transfer fluid in the secondconnecting means and the heat transfer fluid in the third connectingmeans.
 34. The system of claim 32, further comprising means fortransferring heat from the heat transfer fluid in the third connectingmeans to a low temperature heat sink.
 35. The system of claim 33,further comprising means for transferring heat from the heat transferfluid flowing from the auxiliary heat exchanger means in the thirdconnecting means to a low temperature heat sink.
 36. The system of claim32, wherein the primary heating means comprises a heating device betweeneach of the compressors in the train and between the pumping meansoutlet and the inlet to the heat conductive passageway of eachcompressor, the heating devices for heating the heat transfer fluidbefore it is introduced into the compressor of which it is intended, thethusly heated heat transfer fluid thereby heating said compressor.
 37. Aregenerative sorbent heat pump system comprising:a working fluid beingoperable for being sorbed by a sorbent; a plurality of compressors, thenumber of compressors being at least four, each of the compressorshavinga sorbent contained within the compressor, and a heat conductivepassageway having an inlet and an outlet, the heat conductive passagewayfor flowing a heat transfer fluid through the compressor and forindirectly transferring heat between the sorbent and the heat transferfluid without the heat transfer fluid being in contact with the sorbent;means for removing high temperature, high pressure working fluid vaporfrom each of the compressors; condensing means for transferring heatfrom the working fluid to a low temperature heat sink, and, forcondensing working fluid vapor to form a low temperature, high pressureworking fluid liquid; evaporating means for converting low temperature,high pressure working fluid liquid to low temperature, low pressureworking fluid vapor, and, for transferring heat from a low temperaturesource external of the system to the working fluid; liquid conveyingmeans for conveying low temperature, high pressure working fluid liquidfrom the condensing means to the evaporating means; vapor conveyingmeans for conveying low temperature low pressure working fluid vaporinto each of the compressors; a heat transfer fluid; a plurality ofindirect heat exchange means, the number of indirect heat exchange meansbeing equal to the number of the compressors, each of the indirect heatexchange means having a first channel for flowing a primary portion ofthe heat transfer fluid, and a second channel for flowing a secondaryportion of the heat transfer fluid, the channels being isolated fromfluid communication with each other, the first channel being in heatconductive communication with the second channel, each of the channelshaving an inlet and an outlet; a train formed by connecting inalternating order, the first channels of the indirect heat exchangemeans to the heat conductive passageways, the train having an inletwhich is also the inlet of the first channel of the first-in-the-seriesof indirect heat exchange means of the train, and, the train having anoutlet which is also the outlet of the heat conductive passageway of thelast-in-the-series of compressors of the train; first pumping means forpumping the primary portion of a heat transfer fluid around the firsttrain, the outlet of the first pumping means being connected to thetrain inlet and the train outlet being connected to the first pumpingmeans inlet; second pumping means for pumping the secondary portion ofthe heat transfer fluid; connecting means for connecting the outlet ofthe second pumping means to the inlet of the second channel of each ofthe internal heat exchange means, and for connecting the outlet of eachof the second channels thereof to the second pumping means inlet; flowcontrol means for directing the secondary portion of the heat transferfluid from the second pumping means to the second channel of apredetermined one of the indirect heat exchange means in a predeterminedorder thereby defining a flow cycle, and, for enabling heat transferbetween the primary portion of the heat transfer fluid in the firstchannel thereof and the secondary portion of the heat transfer fluid inthe second channel thereof; primary heating means for heating each ofthe compressors; heat control means for controlling the heating periodof the primary heating means in each of the compressors thereby defininga heating cycle; means for transferring heat from the primary portion ofthe heat transfer fluid flowing from the train to a low temperature heatsink; and, heat discharge means for transferring heat rom the secondaryportion of the heat transfer fluid in the connecting means from thesecond channels to the second pump means, to a low temperature heat sinkthereby providing a regenerative sorbent heat pump system.
 38. Thesystem of claim 37, wherein the primary pumping means is also thesecondary pumping means.
 39. The system of claim 37, wherein the primaryheating means comprises a heating device between each of the compressorsin the train and between the first pumping means outlet and the traininlet, the heating devices for heating the first heat transfer fluidbefore it is introduced into the compressor for which it is intended thethusly heated first heat transfer fluid thereby heating said compressor.40. The system of claim 37, further comprising auxiliary heat exchangermeans for indirectly exchanging heat between the primary portion of theheat transfer fluid flowing to the train and the primary portion of theheat transfer fluid flowing from the train.
 41. A regenerative sorbentheat pump system for regeneration of at least a portion of the heat ofadsorption comprising:a working fluid being operable for being sorbed bya sorbent over a predetermined first temperature range thereby producinga heat of adsorption, and for being desorbed from the sorbent over apredetermined second temperature range which is higher than thepredetermined first temperature range, a part of the predetermined firsttemperature range overlapping a part of the predetermined secondtemperature range thereby enabling regeneration of at least a portion ofthe heat of adsorption; a plurality of compressors, the number ofcompressors being at least four, each of the compressors havinga sorbentcontained within the compressor, and a heating conductive passagewayhaving an inlet and an outlet, the heat conductive passageway forflowing a heat transfer fluid through the compressor and for indirectlytransferring heat between the sorbent and the heat transfer fluidwithout the heat transfer fluid being in contact with the sorbent; meansfor removing high temperature, high pressure working fluid vapor fromeach of the compressors; condensing means for transferring heat from theworking fluid to a low temperature heat sink, and, for condensingworking fluid vapor to form a low temperature, high pressure workingfluid liquid; evaporating means for converting low temperature, highpressure working fluid liquid to low temperature, low pressure workingfluid vapor, and, for transferring heat from a low temperature sourceexternal of the system to the working fluid; liquid conveying means forconveying low temperature, high pressure working fluid liquid from thecondensing means to the evaporating means; vapor conveying means forconveying low temperature, low pressure working fluid vapor into each ofthe compressors; first connecting means for forming a loop of heatconductive passageways by connecting the outlet of one heat conductivepassageway to the inlet of another heat conductive passageway andproceeding with such inlet-to-outlet connections until the outlet of thelast heat conductive passageway is connected to the inlet of the firstheat conductive passageway thereby forming a loop of heat conductivepassageways; a heat transfer fluid; pumping means for pumping the a heattransfer fluid; second connecting means for connecting the outlet of thepumping means to the inlet of each of the heat conductive passageways;third connecting means for connecting the outlet of each of the heatconductive passageways to the pumping means inlet; flow control meansfor directing the heat transfer fluid from the pumping means to theinlet of a predetermined one of the heat conductive passageways, thenaround the loop passing through each of the heat conductive passagewaysonly once, and then to the pumping means; phase timing means forredirecting the heat transfer fluid after a predetermined time interval,from the pumping means to another one of the heat conductive passagewaysthereby beginning a new phase, and for repeating such redirecting aftersuch predetermined time intervals to other of the heat conductivepassageways, until the heat transfer fluid is directed from the pumpingmeans to each of the heat conductive passageways thereby completing aflow cycle; primary heating means for heating each of the compressors;heat control means for controlling the heating period of the primaryheating means in each of the compressors; and, heat discharge means fortransferring heat from the heat transfer fluid in the third connectingmeans to a low temperature heat sink thereby providing a regenerativesorbent heat pump system operable for regeneration of at least a portionof the heat of adsorption.
 42. The process of claim 41, wherein theprimary heating means comprises a heating device between each of thecompressors in the loop for heating the heat transfer fluid in the firstconnecting means before the heat transfer fluid is introduced into theheat conductive passageway of the compressor for which it is intendedthereby heating such compressor.
 43. The process of claim 1 furthercomprising, before performing step (i), heating the hottest compressorfurther to a predetermined topping temperature.
 44. The process of claim15 further comprising, before performing step (j), heating the hottestcompressor further to a predetermined topping temperature.
 45. Theprocess of claim 16 further comprising, before performing step (j),heating the hottest compressor further to a predetermined toppingtemperature.
 46. The process of claim 1, wherein the heat transfer fluidis a liquid.
 47. The process of claim 1, wherein the heat transfer fluidis selected from the group consisting of mixtures of diphenyl anddiphenyl oxide, orthodichlorobenzene, ethylene glycol, methoxypropanol,and water.
 48. The process of claim 15, wherein the heat transfer fluidis a liquid.
 49. The process of claim 15, wherein the heat transferfluid is selected from the group consisting of mixtures of diphenyl anddiphenyl oxide, orthodichlorobenzene, ethylene glycol, methoxypropanol,and water.
 50. The process of claim 16, wherein the first heat transferfluid is a liquid.
 51. The process of claim 16, wherein the first heattransfer fluid is selected from the group consisting of mixtures ofdiphenyl and diphenyl oxide, orthodichlorobenzene, ethylene glycol,methoxypropanol, and water.
 52. The process of claim 16, wherein thesecond heat transfer fluid is a liquid.
 53. The process of claim 16,wherein the second heat transfer fluid is selected from the groupconsisting of mixtures of diphenyl and diphenyl oxide,orthodichlorobenzene, ethylene glycol, methoxypropanol, and water. 54.The process of claim 16, wherein the first and second heat transferfluid are liquids.
 55. The process of claim 16, wherein the first andsecond heat transfer fluids are selected from the group consisting ofmixtures of diphenyl and diphenyl oxide, ortho-dichlorobenzene, ethyleneglycol, methoxypropanol, and water.
 56. The system of claim 20, whereinthe first and second heat transfer fluid are liquids.
 57. The system ofclaim 20, wherein the first and second heat transfer fluids are selectedfrom the group consisting of mixtures of diphenyl and diphenyl oxide,ortho-dichlorobenzene, ethylene glycol, methoxypropanol, and water. 58.The process of claim 1, further comprising refrigerant vapor thermalregenerating.
 59. The system of claim 31, further comprising means forrefrigerant vapor thermal regeneration.